Method of Fabricating Fuel Reforming Catalyst for SOFC Power Generating System

ABSTRACT

A fuel reforming catalyst is fabricated. The catalyst is used in solid oxide fuel cell. By using the catalyst, the hydrogen generation is enhanced with a great reforming ratio. In addition, the catalyst is coking-resistant and will not be broken into powder after a long time of use.

TECHNICAL FIELD OF THE INVENTION

The present invention relates to fuel reforming catalyst; more particularly, relates to using α-Al₂O₃ as support for fabricating a catalyst, e.g. Pt/CeO₂/α-Al₂O₃, being coking-resistant and having long life.

DESCRIPTION OF THE RELATED ARTS

Clear green energy is an urgent need today. Solid oxide fuel cell (SOFC) is one solution with its high efficiency and low CO₂ generation. However, SOFC has problems in support powderization and coking after reforming reaction of nickel(Ni)-based catalyst.

Ni has a periodical crystal structure to adhere CH₄ molecules for hydrogen generation by releasing hydrogen atoms. Because the Ni-based catalyst is cheap, it is usually used for reforming reaction in hydrogen reforming generation. Methods for fabricating the Ni-based catalyst include precipitation, co-precipitation and impregnation. The methods of precipitation and co-precipitation are more complex and severer than the method of impregnation on making bearing of support uniform. The method of impregnation uses Ni(NO₃)₃ to be dissolved in water and then porous grains of Al₂O₃ are impregnated in the solution. After drying, the reactants are sintered at a high temperature for resolving Ni(NO₃)₃ to be born in the pores of grains of Al₂O₃. At last, hydrogen is used for reduction to obtain the Ni-based catalyst. In principle, the smaller the grain is, the bigger its activity is. Hence, the catalyst is usually born on an inert material or a material helping the reaction. A good catalyst support can be obtained with Ni born on Al₂O₃. Yet, when the density of Ni is too high, bulk-Ni may be easily formed and the bulk-Ni may be easily accumulated and sintered with activity of the catalyst lost. When there is no bulk-Ni in the catalyst support, a higher density of Ni in the catalyst obtains a better efficiency of the catalyst. Through temperature programmed reduction (TPR), when the density of Ni born in the catalyst is higher, consumption of hydrogen is higher, which means more chains between Ni atoms and Al₂O₃ make distribution of Ni more uniform in the catalyst and the catalyst is less sintered with better hydrogen generation thus obtained. It is found that a catalyst bearing 8.3% of Ni (NiO:10.56%) has a good hydrogen generation. Ni-based catalyst supports have long life times more than 900 hours (hr) and 300 hrs for ones having sizes of millimeters (mm) and 3˜6 mm, respectively. The performances of hydrogen generation of the catalysts are stable in SOFC. Yet, it is also found that the 1 mm and 3˜6 mm catalyst supports are powderized after a reforming reaction at a temperature of about 800 Celsius degrees (° C.).

Generally, the catalyst support is chosen by its specific surface area (effect in distribution of active spots), porous ratio (effect in mass transference and heat transference), grain size (effect in pressure drop) and mechanic strength. Al₂O₃ is the most widely used support as a catalyst. But, NiO and γ-Al₂O₃ would be easily reacted into NiAl₂O₄ at a high-temperature environment filled with oxygen. NiAl₂O₄ is not easily reduced and is inactive, which would affect the characteristics of the catalyst. In FIG. 6, γ-Al₂O₃ having sizes of 1 mm and 3˜6 mm are powderized after sintered at 400° C. It shows that these two Al₂O₃ supports do not fit in high-temperature reforming reaction.

In reforming reactions, traditional catalyst supports may be easily powderized with their activities lost; and gage pressure may be increased owing to coking and powderizing with their performances decreased. Hence, the prior arts do not fulfill all users' requests on actual use.

SUMMARY OF THE INVENTION

The main purpose of the present invention is to use α-Al₂O₃ as support for fabricating a catalyst being coking-resistant and having long life.

To achieve the above purpose, the present invention is a method of fabricating a fuel reforming catalyst for SOFC power generating system, comprising steps of: (a) obtaining γ-Al₂O₃ in a high-temperature furnace with air flown in for processing sintering under a temperature increasing velocity of 5° C. per minute (° C./min) to a temperature of 1080˜1320° C. for a time period of 6˜9 hours (hr); and, then, cooling down the temperature to a room temperature under a temperature decreasing velocity of 5° C./min to obtain a catalyst of α-Al₂O₃; (b) obtaining Ce(NO₃)₃.6H₂O to be dissolved in a de-ionized water to obtain a Ce(NO₃)₃ solution; (c) impregnating the catalyst of α-Al₂O₃ in the Ce(NO₃)₃ solution; (d) taking surplus water of the Ce(NO₃)₃ solution containing the catalyst of α-Al₂O₃ out by a cyclotron vacuum concentrator to obtain CeO₂/α-Al₂O₃; (e) putting CeO₂/α-Al₂O₃ into an oven to be dried; (f) putting CeO₂/α-Al₂O₃ into a high-temperature furnace with air flown in for processing sintering under a temperature increasing velocity of 5° C./min to a temperature of 440˜660° C. for a time period of 3˜5 hrs; (g) obtaining dihydrogen hexachloroplatinate to be dissolved in a de-ionized water to obtain a platinum solution; (h) impregnating CeO₂/α-Al₂O₃ in the platinum solution; (i) taking surplus water out of the platinum solution containing the CeO₂/α-Al₂O₃ by a cyclotron vacuum concentrator to be put into an oven to be dried; and (j) putting the platinum solution containing CeO₂/α-Al₂O₃ in a high-temperature furnace with air flown in for processing sintering under a temperature increasing velocity of 5° C./min to a temperature of 520˜780° C. for a time period of 3˜5 hr; and, then, cooling down the temperature to a room temperature under a temperature decreasing velocity of 5° C./min to obtain a catalyst of Pt/CeO₂/α-Al₂O₃. Accordingly, a novel method of fabricating a fuel reforming catalyst for SOFC power generating system is obtained.

BRIEF DESCRIPTIONS OF THE DRAWINGS

The present invention will be better understood from the following detailed description of the preferred embodiment according to the present invention, taken in conjunction with the accompanying drawings, in which

FIG. 1 is the flow view showing the preferred embodiment according to the present invention;

FIG. 2 is the view showing the crystalline phase of the catalyst supports;

FIG. 3 is the view showing the hydrogen generation densities of the catalysts;

FIG. 4 is the view showing the gas reforming durability;

FIG. 5 is the view showing the gas compositions at the outlet for the hydrogen reforming generation; and

FIG. 6 is the view showing the statuses of the traditional γ-Al₂O₃ before and after sintering.

DESCRIPTION OF THE PREFERRED EMBODIMENT(S)

The following description of the preferred embodiment is provided to understand the features and the structures of the present invention.

Please refer to FIG. 1, which is a flow view showing a preferred embodiment according to the present invention. As shown in the figure, the present invention is a method of fabricating a fuel reforming catalyst for solid oxide fuel cell (SOFC) power generating system, where catalysts of Ni/CeO₂/α-Al₂O₃ and Pt/CeO₂/α-Al₂O₃ for hydrogen reforming generation are obtained. In a state of use, for fabricating 40 grams (g) of 2% Pt/10% CeO₂/α-Al₂O₃, the present invention comprises the following steps:

(a1) Obtaining α-Al₂O₃ 11: γ-Al₂O₃ is put into a high-temperature furnace with 3LPM of air flown in. Then, γ-Al₂O₃ is sintered under a temperature increasing velocity of 5 Celsius degrees per minute (° C./min) to a temperature of 1200° C. for a time period of 8 hours (hr). Then, the temperature is cooled down to a room temperature under a temperature decreasing velocity of 5° C./min to obtain grains of a catalyst support of α-Al₂O₃.

(b1) Obtaining Ce(NO₃)₃ solution 12: 18.6 g of Ce(NO₃)₃.6H₂O is obtained to be dissolved in a de-ionized water to obtain a Ce(NO₃)₃ solution.

(c1) Impregnating 13: (c) The 40 g catalyst support of α-Al₂O₃ is impregnated in the Ce(NO₃)₃ solution for 12 hrs.

(d1) Taking off water 14: Surplus water of the Ce(NO₃)₃ solution containing grains of the catalyst support of α-Al₂O₃ is taken out by a cyclotron vacuum concentrator to obtain CeO₂/α-Al₂O₃.

(e1) Drying 15: CeO₂/α-Al₂O₃ obtained after taking out surplus water is put into an oven to be dried at a temperature of 110° C. for 24 hrs.

(f1) Sintering 16: CeO₂/α-Al₂O₃ is put into a high-temperature furnace with 3PLM of air flown in to be sintered under a temperature increasing velocity of 5° C./min to a temperature of 550° C. for a time period of 4 hrs.

(g1) Obtaining platinum solution 17: 21.25 g of dihydrogen hexachloroplatinate is obtained to be dissolved in 50 g of a de-ionized water to obtain a platinum solution.

(h1) Impregnating 18: 40 g of CeO₂/α-Al₂O₃ is obtained to be impregnated in the platinum solution for 12 hrs.

(i1) Taking out water and drying 19: Surplus water of the platinum solution containing CeO₂/α-Al₂O₃ is taken out by a cyclotron vacuum concentrator to be put into an oven to be dried at a temperature of 110° C. for 24 hrs.

(j1) Obtaining Pt/CeO₂/α-Al₂O₃ 20: The platinum solution containing CeO₂/α-Al₂O₃ is put in a high-temperature furnace with air flown in to be sintered under a temperature increasing velocity of 5° C./min to a temperature of 650° C. for a time period of 4 hr. Then, the temperature is cooled down to a room temperature under a temperature decreasing velocity of 5° C./min to obtain a catalyst of Pt/CeO₂/α-Al₂O₃.

In another state of use, for fabricating 40 g of 8.3% Ni/10% CeO₂/α-Al₂O₃, the present invention comprises the following steps:

(a2) γ-Al₂O₃ is put into a high-temperature furnace with 3LPM of air flown in. Then, γ-Al₂O₃ is sintered under a temperature increasing velocity of 5° C./min to a temperature of 1200° C. for a time period of 8 hrs. Then, the temperature is cooled down to a room temperature under a temperature decreasing velocity of 5° C./min to obtain grains of a catalyst support of α-Al₂O₃.

(b2) 18.6 g of Ce(NO₃)₃.6H₂O is obtained to be dissolved in a de-ionized water to obtain a Ce(NO₃)₃ solution.

(c2) The 40 g catalyst support of α-Al₂O₃ is impregnated in the Ce(NO₃)₃ solution for 12 hrs.

(d2) Surplus water of the Ce(NO₃)₃ solution containing grains of the catalyst support of α-Al₂O₃ is taken out by a cyclotron vacuum concentrator to obtain CeO₂/α-Al₂O₃.

(e2) CeO₂/α-Al₂O₃ obtained after taking out surplus water is put into an oven to be dried at a temperature of 110° C. for 24 hrs.

(f2) CeO₂/α-Al₂O₃ is put into a high-temperature furnace with 3PLM of air flown in to be sintered under a temperature increasing velocity of 5° C./min to a temperature of 550° C. for a time period of 4 hrs.

(g2) 21.25 g of Ni(NO₃)₃.6H₂O is obtained to be dissolved in 50 g of a de-ionized water to obtain a Ni(NO₃)₃ solution.

(h2) 40 g of CeO₂/α-Al₂O₃ is obtained to be impregnated in the Ni(NO₃)₃ solution for 12 hrs.

(i2) Surplus water of the Ni(NO₃)₃ solution containing CeO₂/α-Al₂O₃ is taken out by a cyclotron vacuum concentrator to be put into an oven to be dried at a temperature of 110° C. for 24 hrs.

(j2) The Ni(NO₃)₃ solution containing CeO₂/α-Al₂O₃ is put in a high-temperature furnace with air flown in to be sintered under a temperature increasing velocity of 5° C./min to a temperature of 650° C. for a time period of 4 hr. Then, the temperature is cooled down to a room temperature under a temperature decreasing velocity of 5° C./min to obtain a catalyst of Ni/CeO₂/α-Al₂O₃.

Since the reforming reaction by catalyst may make the catalyst become inactive owing to the support used, γ-Al₂O₃ is made into the crystalline phase of α-Al₂O₃ at a temperature of 1200° C. for reducing the possibility of forming spinels of NiAl₂O₄.

Please refer to FIG. 2, which is a view showing crystalline phase of catalyst supports. As shown in the figure, curves of crystalline phase of catalyst supports are obtained through X-ray diffraction (XRD). The first curve 21 shows the XRD curve of α-Al₂O₃ obtained through the present invention. The second and the third curves 22,23 shows the XRD curves of traditional 1 mm and 3-6 mm Ni-based catalysts of γ-Al₂O₃. In the figures, the curves of the traditional catalysts are almost the same regardless of their sizes. But, the curve of the α-Al₂O₃ obtained through the present invention shows a more obvious peak, which proves to be a better support.

Please refer to FIG. 3 and FIG. 5, which are a view showing the hydrogen generation densities of the catalysts; and a view showing gas compositions at outlet for hydrogen reforming generation. As shown in the figures, two catalysts of Ni/CeO₂/α-Al₂O₃ and Pt/CeO₂/α-Al₂O₃ and a traditional catalyst are obtained for testing reforming reaction through autothermal reaction. Reactants including CH₄, air and water (H₂O) are mixed for hydrogen generation with the catalysts by reforming reaction at a high temperature. The ratios of H₂O/CH₄ and O/C are fixed. The reaction is processed with the following conditions: the ratios of H₂O/CH₄ and O/C are H₂O/CH₄=2, O/C=0.35, respectively; the reaction temperature is about 780˜800° C.; and the air is flown in a velocity about 2.5 L/g-h. The traditional catalyst made of Pt, Rh and Pd is obtained. Because the honeycomb is cut into accumulation of large particles with more interspace, the residence time for the reactants may be short to result in incomplete reaction. Hence, in 120 minutes (min) for reforming reaction, a first hydrogen generation curve 31 for the catalyst of Pt—Rh—Pd shows a lower hydrogen density at gas generating outlet. Instead, the other two catalysts of Ni/CeO₂/α-Al₂O₃ and Pt/CeO₂/α-Al₂O₃ have longer residence times owing to an irregular stacking of grains although the α-Al₂O₃ support used has a small specific surface area. In the 120 min for reforming reaction, the second and the third hydrogen generation curves 32,33 for the catalysts of Ni/CeO₂/α-Al₂O₃ and Pt/CeO₂/α-Al₂O₃ shows hydrogen densities higher than 68% at gas generating outlet with no obvious declining tendency. In FIG. 5, the traditional catalyst has lower hydrogen generation density and gas compositions at the outlet contain about 4% CH₄. But, the catalysts of Ni/CeO₂/α-Al₂O₃ and Pt/CeO₂/α-Al₂O₃ have no CH₄ at the outlet, which shows 99% CH₄ conversion rate. Hence, the catalysts of Ni/CeO₂/α-Al₂O₃ and Pt/CeO₂/α-Al₂O₃ fabricated according to the present invention have higher activities on hydrogen generation.

Please refer to FIG. 4, which is a view showing gas reforming durability. As shown in the figure, a reforming catalyst is used for SOFC. The reforming catalyst is not powderized after being used for 1000 hrs and keep none-coking or active. Hence, the reforming catalyst using α-Al₂O₃ support is coking-resistant and has long life.

The reforming catalysts fabricated through the present invention uses α-Al₂O₃ as support for high-temperature resistance and good hardness. The catalysts of Pt/CeO₂/α-Al₂O₃ and Ni/CeO₂/α-Al₂O₃ thus fabricated have good performances for hydrogen generation, where the hydrogen generation density reaches about 68% after 120 min with a conversion rate higher than 99%; and the catalysts all have a resistance to be used more than 1000 hrs.

To sum up, the present invention is a method of fabricating a fuel reforming catalyst for SOFC power generating system, where α-Al₂O₃ is used as support with high-temperature resistance and good hardness; the catalysts of Pt/CeO₂/α-Al₂O₃ and Ni/CeO₂/α-Al₂O₃ thus fabricated have good performance for hydrogen generation; the hydrogen generation density reaches about 68% after 120 min with a conversion rate higher than 99%; and the catalysts is coking-resistant and has long life.

The preferred embodiment herein disclosed is not intended to unnecessarily limit the scope of the invention. Therefore, simple modifications or variations belonging to the equivalent of the scope of the claims and the instructions disclosed herein for a patent are all within the scope of the present invention. 

What is claimed is:
 1. A method of fabricating a fuel reforming catalyst for solid oxide fuel cell (SOFC) power generating system, comprising steps of: (a) obtaining γ-Al₂O₃ in a high-temperature furnace with air flown in to be sintered under a temperature increasing velocity of 5 Celsius degrees per minute (° C./min) to a temperature of 1080˜1320° C. for a time period of 6˜9 hours (hr); and, then, cooling down said temperature to a room temperature under a temperature decreasing velocity of 5° C./min to obtain a catalyst of α-Al₂O₃; (b) obtaining Ce(NO₃)₃.6H₂O to be dissolved in a de-ionized water to obtain a Ce(NO₃)₃ solution; (c) impregnating said catalyst of α-Al₂O₃ in said Ce(NO₃)₃ solution; (d) taking surplus water of said Ce(NO₃)₃ solution containing said catalyst of α-Al₂O₃ out by a cyclotron vacuum concentrator to obtain CeO₂/α-Al₂O₃; (e) putting CeO₂/α-Al₂O₃ into an oven to be dried; (f) putting CeO₂/α-Al₂O₃ into a high-temperature furnace with air flown in to be sintered under a temperature increasing velocity of 5° C./min to a temperature of 440˜660° C. for a time period of 3˜5 hrs; (g) obtaining dihydrogen hexachloroplatinate to be dissolved in a de-ionized water to obtain a platinum solution; (h) impregnating CeO₂/α-Al₂O₃ in said platinum solution; (i) taking surplus water out of said platinum solution containing CeO₂/α-Al₂O₃ by a cyclotron vacuum concentrator to be put into an oven to be dried; and (j) putting said platinum solution containing CeO₂/α-Al₂O₃ in a high-temperature furnace with air flown in to be sintered under a temperature increasing velocity of 5° C./min to a temperature of 520˜780° C. for a time period of 3˜5 hr; and, then, cooling down said temperature to a room temperature under a temperature decreasing velocity of 5° C./min to obtain a catalyst of Pt/CeO₂/α-Al₂O₃.
 2. The method according to claim 1, wherein said catalyst of Pt/CeO₂/α-Al₂O₃ has a resistance over 1000 hrs and a conversion higher than 99%.
 3. The method according to claim 1, wherein, in step (a), 3LPM of air is flown in to process sintering under a temperature increasing velocity of 5° C./min to a temperature of 1200° C. for a time period of 8 hrs.
 4. The method according to claim 1, wherein, in step (c), said impregnating is processed for 12 hrs.
 5. The method according to claim 1, wherein, in step (f), 3LPM of air is flown in to process sintering under a temperature increasing velocity of 5° C./min to a temperature of 550° C. for a time period of 4 hrs.
 6. The method according to claim 1, wherein, in step (h), said impregnating is processed for 12 hrs.
 7. The method according to claim 1, wherein, in step (j), 3LPM of air is flown in to process sintering under a temperature increasing velocity of 5° C./min to a temperature of 650° C. for a time period of 4 hrs.
 8. The method according to claim 1, wherein said catalyst of α-Al₂O₃ has a cylinder shape with a diameter of 3 millimeters (mm).
 9. The method according to claim 1, wherein dihydrogen hexachloroplatinate in step (g) is replaced with Ni(NO₃)₃.6H₂O to obtain Ni/CeO₂/α-Al₂O₃ in step (j). 